Search Images Maps Play YouTube News Gmail Drive More »
Sign in
Screen reader users: click this link for accessible mode. Accessible mode has the same essential features but works better with your reader.

Patents

  1. Advanced Patent Search
Publication numberUS4289612 A
Publication typeGrant
Application numberUS 06/158,380
Publication dateSep 15, 1981
Filing dateJun 11, 1980
Priority dateJun 11, 1980
Also published asCA1130017A1
Publication number06158380, 158380, US 4289612 A, US 4289612A, US-A-4289612, US4289612 A, US4289612A
InventorsGlenn H. Schrieber
Original AssigneeTexasgulf Inc.
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Phosphate ore triple float
US 4289612 A
Abstract
A process for the improved beneficiation of phosphate ore in which the double float cationic (i.e., amine) floatation step is performed in two stages instead of the standard single stage, and which permits recovery of approximately two-thirds of the phosphate values that were previously lost in the amine tailings of the standard single stage process.
Images(1)
Previous page
Next page
Claims(5)
I claim:
1. An improved process for the beneficiation of phosphate ore wherein the ore is floated with anionic reagent to produce a single float product, the single float product is treated with acid to remove anionic reagent, and the acid treated single float product is subjected to cationic floatation with cationic reagent to produce a double float product, wherein the improvement comprises:
(a) performing said cationic floatation in first and second stages;
(b) adding cationic floatation reagent in starvation amounts in said first stage with a low floatation retention time to produce a float containing most of the silica from the ore which is discarded; and,
(c) adding additional cationic floatation reagent to the phosphate ore remaining from said first stage to said second stage with enough floatation retention time to produce a float containing most of the phosphate from the total cationic floatation tailings which is recovered.
2. An improved process according to claim 1, wherein said low floatation retention time is about one-third the normal time for cationic floatation.
3. An improved process according to claim 1, wherein the cationic floatation tailings from said second stage is mixed with a separate single float product.
4. An improved process according to claim 1, wherein the cationic floatation product from said second stage is used as a traditional double float product.
5. An improved process according to claim 1, wherein the amount of cationic floatation reagent added to said first and said second stage is approximately equal in volume to the amount of cationic floatation reagent added to a traditional double float process.
Description
BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates to a process for beneficiating phosphate ore, and, more particularly, to a process by which phosphate ore can be beneficiated with improved recovery in the cationic floatation step.

2. Description of the Prior Art

A standard method for the beneficiation of phosphate ore is called "double float". The phosphate ore is first floated with any of one or more of several well-known anionic reagents (i.e., fatty acids), which leaves the rougher tailings low in phosphate values. This "single float" product still contains some silica, which is then scrubbed with sulfuric acid to remove the reagents and then subjected to floatation using any of one or more of several well-known cationic reagents (i.e., amines). The majority of the remaining silica is floated away, leaving a "double float" product high in phosphate values and very low in silica. The tailings (i.e., silica component) from the amine floatation still contain more phosphate values than is desireable to discard as waste, but the values are not great enough to be utilized as a product.

I have now discovered that it is possible to recover approximately two-thirds of the phosphate values that were previously lost in the amine tailings.

These lost phosphate values are recovered by modifying the standard "double float" process to a "triple float" process by removing the tailings in the amine float in two stages instead of one, and, surprisingly, this is accomplished with approximately the same volume of amine reagent currently utilized in the "double float" process.

SUMMARY OF THE INVENTION

An improved process for the beneficiation of phosphate ore wherein the ore is floated with anionic reagent to produce a single float product, the single float product is treated with acid to remove anionic reagent, and the acid treated single float product is floated with cationic reagent to produce a double float product, wherein the improvement comprises:

(a) performing said cationic floatation in first and second stages;

(b) adding cationic floatation reagent in starvation amounts in said first stage with a low floatation retention time to produce a float containing most of the silica from the ore which is discarded; and,

(c) adding additional cationic floatation reagent to the phosphate ore remaining from said first stage to said second stage with a sufficient floatation retention time to produce a float containing most of the phosphate from the amine tailings which is recovered.

A preferred embodiment of the instant invention comprises utilizing a cationic floatation reagent selected from the group comprising Natrochem Inc. JJ-95, Westvaco Inc. Custamine 705 and AZ Products Inc. A-33A.

A second preferred embodiment of the instant invention comprises utilizing a first stage low floatation retention time of about one-third the normal time for cationic floatation.

A third preferred embodiment of the instant invention is mixing the cationic floatation tailings from the second stage with an entirely separate single float product.

A fourth preferred embodiment of the instant invention is utilizing the cationic floatation product from the second stage as a traditional double float product.

A fifth preferred embodiment of the instant invention is utilizing approximately the same amount of cationic floatation reagent in the first and second stages as used in a traditional double float process.

BRIEF DESCRIPTION OF THE DRAWING

The FIG. is a schematic diagram illustrating a flowsheet useful in carrying out the invention.

DESCRIPTION OF THE PREFERRED EMBODIMENT

In order to achieve the maximum benefit from this "triple float" process, it may be desireable for a phosphate ore manufacturer to have a use for a secondary, or lower grade, product as well as the traditional "double float" product. The lower grade product may consist of phosphate ore that has been processed with only an anionic floatation step, traditionally referred to as a "single float" product, which is then mixed with the instant second stage floatation tailings.

Reference is now made to the FIG., in which a simplified schematic representation of a flowsheet for beneficiating phosphate ore by a "triple float" process is shown. In the description which follows, as in the FIG., supporting structure which would be conventionally supplied has been omitted in the interest of simplicity of presentation. It will therefore be understood that sized and de-slimed phosphate ore can be beneficiated by a single float process or by a double float process. In both the single and double float processes the same anionic (i.e., fatty acid) reagents are utilized. Typical anionic reagents are Union Camp CTF, Westvaco Inc. Liqro T and Arizona Chemicals Co. FA 140. The phosphate values are floated with the anionic reagent, leaving the rougher tailings low in phosphate. In both the single and double float processes the phosphate rich component is then scrubbed with an acid, preferably sulfuric acid, to remove (i.e., de-oil) the anionic reagents. After deoiling, the single float product can be utilized, if desired, without further processing. To produce a double float product, a further cationic floatation step is required.

As indicated on the FIG., I have discovered that it is possible to recover approximately two-thirds (66%) of the phosphate values lost by the traditional double float method by performing the cationic floatation step in two, instead of one, stages. The same cationic (i.e., amine) reagents used for the double float are also used in the instantly claimed triple float process. Typical cationic reagents are Natrochem Inc. JJ-95, Westvaco Inc. Custamine 705 and AZ Products Inc. A-33A. It should be noted that approximately the same plume of cationic reagent is used in both the double float and triple float process.

The amine flotation reagents are compositions containing a cationic nitrogen group and a hydrophobic chain. Therefore, stearyl amine and tallow amine are suitable for this purpose. To achieve good water dispersability, acetates of these amines are advantageously used. However, these long chain fatty amines and their acetate salts are not too selective in floating sand; some phosphate ore particles are also lost in the process. In order to reduce this phosphate loss, a composition prepared from the condensation of polyalkylene polyamine and a fatty acid is advantageously used. Thus, diethylene triamine is reacted with tall oil fatty acid to produce a reagent containing one cationic nitrogen group and two fatty amide groups. Better water dispersability is achieved by using the acetate salt of the diethylene triamine fatty acid reaction product. A much preferred product for flotation is a mixture of the tallow amine acetate and polyalkylene polyamine fatty acid acetate. Examples of the fatty acid are myristic, oleic, stearic, palmitic, isostearic, soybean, tallow, lard, tall oil, caster and the like. Examples of polyalkylene polyamines are diethylene, triamine, triethylene, tetramine, 3-3 iminobispropylamine, and the like.

The triple float process requires that the cationic floatation be performed in two stages. In the first stage, cationic reagent is added in starvation amounts and the floatation retention time is low (i.e., about one-third the time required for traditional cationic floation). The combination of starvation amounts of cationic reagent and low floatation retention time results in amine tailings (i.e., the floated ore) that contains most of the silica from the feed but very little phosphate. The amine tailings from the first stage are discarded. The product from this first stage treatment is not the final grade product. The product from the first stage is then subjected to the second stage of floatation with additional cationic reagent. This second stage requires that additional cationic floatation reagent be added to the phosphate ore remaining from said first stage with enough floatation retention time to produce a float material (i.e., recovered amine tails) containing most of the phosphate values from the amine tailings. The product from the second stage can be utilized as a traditional double float product.

The following table is included to illustrate the expected increased amount of recovered phosphate values, utilizing a hypothetical one hundred thousand tons of phosphate ore that has first been sized and de-slimed before being subjected to the triple float two stage cationic reagent floatation process.

______________________________________THEORETICAL MATERIAL BALANCE       Tons   % P205     Tons P205______________________________________14 × 200 Mesh Ore         100,000  16.93      16,931.7Float Feed,Single Float  73,696   16.94      12,484.9Float Feed,Triple Float  26,304   16.91      4,446.9Fatty Acid Tails,Single Float  31,672    2.29      926.7Fatty Acid Tails,Triple Float  11,052    2.66      293.8Fatty Acid Conc.,Single Float  42,024   27.50      11,558.1Fatty Acid Conc.,Triple Float  15,253   27.23      4,153.0Amine Tails,Triple Float Total          2,465   11.20      276.1Amine TailsTo Single Float           956    19.46      186.1Amine Tails to Waste          1,508    5.97      90.0Amine Concentrate         12,788   30.32      3,877.0Single Float TonsTo Pile       42,980   27.32      11,744.2Triple Float TonsTo Pile       12,788   30.32      3,877.0______________________________________

The following example is presented to further describe and illustrate the process of this invention.

EXAMPLE

A sample of North Carolina phosphate ore is floated with an anionic reagent to produce a single float product, the single float product is treated with acid to remove anionic reagent, and the acid treated single float product is then floated with cationic reagent in first and second stages to produce a triple float product. The cationic flotation reagent, which is a mixture of Natrochem Inc. JJ-95, Westvaco Inc. Custamine 705, AZ Products Inc. A-33A and No. 2 fuel oil, is added in starvation amounts in the first stage with a low flotation retention time to produce a float containing most of the silica from the ore which is discarded. Additional cationic flotation reagent is added to the phosphate ore remaining from the first stage to the second stage with a sufficient flotation retention time to produce a float containing most of the phosphate from the amine tailings which is recovered. A representative amount of cationic reagent added is as follows:

______________________________________    Amine        No. 2 Fuel Oil______________________________________First Stage      0.83           0.54 (estimate)Second Stage      0.69           0.54 (estimate)Total      1.52           1.08 (actual)______________________________________

The numbers shown above are pounds of reagent per ton of final high grade product. The amine is added as a ten percent (10%) solution in water, and the pounds per ton refer to pure amine and not amine solution. The No. 2 Fuel Oil is not diluted.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2614692 *Jun 8, 1948Oct 21, 1952Int Minerals & Chem CorpRecovery of metallic minerals from phosphate-silica ores containing minor amounts of the metallic minerals
US2676705 *Dec 27, 1951Apr 27, 1954Attapulgus Minerals & ChemicalConcentration of phosphate ores
US2706558 *Feb 4, 1954Apr 19, 1955Minerals & Chemicals CorpConcentration of phosphate minerals
US2750036 *Mar 16, 1954Jun 12, 1956Minerals & Chemicals Corp Of AProcess for concentrating phosphate ores
US2914173 *Jul 19, 1957Nov 24, 1959Int Minerals & Chem CorpMethod of processing phosphate ore to recover metallic minerals
US3013664 *Aug 6, 1959Dec 19, 1961Smith Douglass Company IncBeneficiation of phosphate rock
US3419140 *May 11, 1966Dec 31, 1968Basic IncSelective flotation of dolomite away from magnesite
US4189103 *Mar 10, 1978Feb 19, 1980International Minerals & Chemical CorporationMethod of beneficiating phosphate ores
US4220523 *Jul 19, 1978Sep 2, 1980Jacobs Engineering Group Inc.Recovering of phosphates from phosphate ore
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US4460460 *Apr 13, 1982Jul 17, 1984Mobil Oil CorporationBeneficiation of ores
US4648966 *Dec 2, 1985Mar 10, 1987Tennessee Valley AuthorityProcess for beneficiation of dolomitic phosphate ores
US6685027 *Aug 9, 2001Feb 3, 2004Arr-Maz Products, LpMethod of concentrating phosphates from their ores
CN102245504BDec 11, 2009Nov 6, 2013马克斯ˇ普朗克科学促进协会Phosphate based compound, use of the compound in an electrochemical storage device and methods for its preparation
EP2196434A1 *Dec 12, 2008Jun 16, 2010Max-Planck-Gesellschaft zur Förderung der Wissenschaften e.V.Phosphate based compound, use of the compound in an electrochemical storage device and methods for its preparation
WO2010066439A2 *Dec 11, 2009Jun 17, 2010MAX-PLANCK-Gesellschaft zur Förderung der Wissenschaften e.V.Phosphate based compound, use of the compound in an electrochemical storage device and methods for its preparation
Classifications
U.S. Classification209/166, 209/5
International ClassificationB03D1/02
Cooperative ClassificationB03D1/06, B03D1/021
European ClassificationB03D1/02B
Legal Events
DateCodeEventDescription
May 15, 1981ASAssignment
Owner name: TEXASGULF INC., HIGH RIDGE PARK, STAMFORD, CT., 06
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:SCHRIEBER GLENN H.;REEL/FRAME:003853/0199
Effective date: 19800604
May 10, 1982ASAssignment
Owner name: E A DEVELOPMENT, INC.
Free format text: MERGER;ASSIGNOR:TEXASGULF INC. (MERGED INTO);REEL/FRAME:004019/0954
Effective date: 19820226
Owner name: TEXASGULF INC.
Free format text: CHANGE OF NAME;ASSIGNOR:TEXAS GULF SULPHUR COMPANY;REEL/FRAME:004019/0926
Effective date: 19820415
Owner name: TEXASGULF INC., A CORP. OF TX
Free format text: MERGER;ASSIGNOR:E A DEVELOPMENT, INC.;REEL/FRAME:004019/0947
Effective date: 19820226
Owner name: E A DEVELOPMENT, INC., UNITED STATES
Owner name: E A DEVELOPMENT, INC., UNITED STATES
Free format text: MERGER;ASSIGNOR:TEXASGULF INC. (MERGED INTO);REEL/FRAME:004019/0954
Effective date: 19820226